Preparation of fluorinated olefins via catalytic dehydrohalogenation of halogenated hydrocarbons

ABSTRACT

A process for making a fluorinated olefin having the step of dehydrochlorinating a hydrochlorofluorocarbon having at least one hydrogen atom and at least one chlorine atom on adjacent carbon atoms, preferably carried out in the presence of a catalyst selected from the group consisting of (i) one or more metal halides, (ii) one or more halogenated metal oxides, (iii) one or more zero-valent metals/metal alloys, (iv) a combination of two or more of the foregoing.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a division of U.S. application Ser. No. 12/167,159, filed Jul. 2, 2008 (now U.S. Pat. No. 9,040,759, issued May 26, 2015), which application claims priority to, and incorporates by reference, U.S. Provisional Application No. 60/958,468, filed Jul. 6, 2007.

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates to the dehydrohalogenation of a halogen-containing compound. The present invention further relates to the dehydrochlorination of a hydrochlorofluorocarbon to a fluorinated olefin.

2. Description of the Related Art

Chlorine-containing compounds, such as chlorofluorocarbons (CFCs), have been employed as refrigerants, foam blowing agents, cleaning agents, solvents, heat transfer media, sterilants, aerosol propellants, dielectrics, fire extinguishing agents, and power cycle working fluids. However, CFCs have proven to be detrimental to the Earth's ozone layer. Conventional substitutes for CFCs include hydrofluorocarbons (HFCs); however, these compounds have been found to contribute to global warming. For these reasons, there is a worldwide effort to develop new compounds that are environmentally benign.

Partly or fully fluorinated olefins, including hydrofluoroolefins, (collectively referred to hereinafter as fluorinated olefins) are potential replacements for HFCs and CFCs. They can be used in some of the aforementioned applications and can also be used as feedstock monomers to synthesize fluoropolymers and other macromolecular compounds.

Various methods for producing certain fluorinated olefins are known, including those involving the dehydrochlorination of hydrochlorofluorocarbons. For example, U.S. patent application Ser. No. 11/619,592 discloses a method for preparing 2,3,3,3-tetrafluoropropene (1234yf) via dehydrochlorination of 1,1,1,2-tetrafluoro-2-chloropropane (244bb) with the aid of a catalyst. The 244bb reactant can be prepared through liquid phase or gas phase catalytic fluorination of 1,1,1-trifluoro-2-chloropropene (1233xf) with HF and 1233xf, in turn, can be made via gas phase fluorination of CCl₂═CClCH₂Cl (1,1,2,3-tetrachloropropene) with HF. The '592 application also teaches the use of a carbon- and/or metal-based catalyst for the conversion of 244bb to 1234yf. Depending on the reaction conditions, the conversion of 244bb could be as high as 98%, but has a selectivity for 1234yf of only 69% to 86%. Thus, there remains a need to develop a commercially viable catalyst that not only is active, but also is more selective for 1234yf.

However, the conversion of a hydrochlorofluorocarbon to a fluorinated olefin by conventional methods is problematic because by-products often form and undergo a competing dehydrofluorination reaction. Hence, it would be advantageous to develop a catalyst system that can suppress undesirable dehydrofluorination reactions, so that single-pass productivity and yield of the desired fluorinated olefin can be increased.

SUMMARY OF THE INVENTION

According to the present invention, provided a process for making a fluorinated olefin via dehydrochlorination of a hydrochlorofluorocarbon having at least one hydrogen atom and at least one chlorine atom on adjacent carbon atoms. The dehydrochlorination is carried out in the presence of a catalyst selected from the group consisting of (i) one or more metal halides, (ii) one or more halogenated metal oxides, (iii) one or more zero-valent metals/metal alloys, and (iv) a combination of two or more of the foregoing. Preferred fluorinated olefin products are the following: 2,3,3,3-tetrafluoropropene (1234yf), 1,3,3,3-tetrafluoropropene (trans/cis-1234ze), 1,2,3,3,3-pentafluoropropene (Z/E-1255ye), 1,1,3,3,3-pentafluoropropene (1225zc), and 1,1,2,3,3,3-hexafluoropropene (1216).

DETAILED DESCRIPTION OF THE INVENTION

In the present invention, a hydrochlorofluorocarbon having at least one hydrogen and at least one chlorine on adjacent carbons is dehydrochlorinated in the presence of a catalyst to form a product having a fluorinated olefin therein. Table 1 sets forth examples of fluorinated olefins and precursor hydrochlorofluorocarbons from which they can be obtained (i.e., hydrochlorofluorocarbon in left column and corresponding fluorinated olefin in the right column).

TABLE 1 Hydrochlorofluorocarbon Fluorinated olefin(s) chlorotetrafluoropropane tetrafluoropropene chloropentafluoropropane pentafluoropropene chlorohexafluoropropane hexafluoropropene 1,1,1,2-tetrafluoro-2-chloropropane 2,3,3,3-tetrafluoropropene CF₃CFClCH₃ (244bb) CF₃CF═CH₂ (1234yf) 1,1,1,2-tetrafluoro-3-chloropropane 2,3,3,3-tetrafluoropropene CF₃CHFCH₂Cl (244eb) CF₃CF═CH₂ (1234yf) 1,1,1,3-tetrafluoro-3-chloropropane 1,3,3,3-tetrafluoropropene CF₃CH₂CHFCl (244fa) CF₃CH═CHF (trans/cis-1234ze) 1,1,1,3-tetrafluoro-2-chloropropane 1,3,3,3-tetrafluoropropene CF₃CHClCH₂F (244db) CF₃CH═CHF (trans/cis-1234ze) 1,1,1,2,3-pentafluoro-2-chloropropane 1,2,3,3,3-pentafluoropropene CF₃CFClCH₂F (235bb) CF₃CF═CHF (Z/E-1225ye) 1,1,1,2,3-pentafluoro-3-chloropropane 1,2,3,3,3-pentafluoropropene CF₃CHFCHFCl (235ea) CF₃CF═CHF (Z/E-1225ye) 1,1,1,3,3-pentafluoro-3-chloropropane 1,1,3,3,3-pentafluoropropene CF₃CH₂CF₂Cl (235fa) CF₃CH═CF₂ (1225zc) 1,1,1,3,3-pentafluoro-2-chloropropane 1,1,3,3,3-pentafluoropropene CF₃CHClCHF₂ (235da) CF₃CH═CF₂ (1225zc) 1,1,1,2,3,3-hexafluoro-2-chloropropane 1,1,2,3,3,3-hexafluoropropene CF₃CFClCHF₂ (226ba) CF₃CF═CF₂ (1216) 1,1,1,2,3,3-hexafluoro-3-chloropropane 1,1,2,3,3,3-hexafluoropropene CF₃CHFCF₂Cl (226ea) CF₃CF═CF₂ (1216)

In the process of the present invention, selected catalysts are employed to enhance the selectivity and/or conversion of hydrochlorofluorocarbons to fluorinated olefins. The catalysts are more selective for the dehydrochlorination reaction, which produces fluorinated olefin, than for the competing dehydrofluorination side reaction, which produces the undesirable byproduct chlorine-containing olefin.

There are three preferred classes of catalysts useful in the present invention: (i) metal halides, (ii) halogenated metal oxides, and (iii) zero-valent metals/metal alloys.

The first class of catalysts is metal halides, preferably mono-, bi-, and tri-valent metal halides and their mixtures/combinations, and more preferably mono- and bi-valent metal halides and their mixtures/combinations. Component metals include, but are not limited to, Cr³⁺, Fe³⁺, Mg²⁺, Ca²⁺, Ni²⁺, Zn²⁺, Pd²⁺, Li⁺, Na⁺, K⁺, and Cs⁺. Component halogens include, but are not limited to, F⁻, Cl⁻, Br⁻, and I⁻. Examples of useful mono- or bi-valent metal halide include, but are not limited to, LiF, NaF, KF, CsF, MgF₂, CaF₂, LiCl, NaCl, KCl, and CsCl. The catalyst may be supported or unsupported. A preferred catalyst is a CsCl/MgF₂ combination. A particularly preferred catalyst is a CsCl/MgF₂ combination wherein CsCl is present in an amount of about 5.0 to about 50 wt % based on the total weight of the catalyst.

The second class of catalysts is halogenated metal oxides, preferably halogenated mono-, bi-, and tri-valent metal oxides and their mixtures/combinations, and more preferably halogenated mono- and bi-valent metal oxides and their mixtures/combinations. Component metals include, but are not limited to, Cr³⁺, Fe³⁺, Mg²⁺, Ca²⁺, Ni²⁺, Zn²⁺, Pd²⁺, Li⁺, Na⁺, K⁺, and Cs⁺. Halogenation treatments can include any of those known in the prior art, particularly those that employ HF, F₂, HCl, Cl₂, HBr, Br₂, HI, and I₂ as the halogenation source. Examples of useful halogenated mono- and bi-valent metal oxides include, but are not limited to, fluorinated or chlorinated MgO, fluorinated or chlorinated CaO, fluorinated or chlorinated Li₂O, fluorinated or chlorinated Na₂O, fluorinated or chlorinated K₂O, and fluorinated or chlorinated Cs₂O. The catalyst may be supported or unsupported.

The third class of catalysts is neutral (i.e., zero valent) metals, metal alloys, and their mixtures. Useful metals include, but are not limited to, Pd, Pt, Rh, Fe, Co, Ni, Cu, Mo, Cr, Mn, and combinations of the foregoing as alloys or mixtures. The catalyst may be supported or unsupported. Useful examples of metal alloys include, but are not limited to, SS 316, Monel 400, Inconel 825, Inconel 600, and Inconel 625.

In addition to the fluorinated olefin, i.e., the hydrofluorocarbon or fluorocarbon, the product mixture may also have unconverted hydrochlorofluorocarbon and hydrogen chloride.

Enhanced or improved selectivity for the target product is an important feature of the present invention. The dehydrochlorination reaction is preferably carried out at a selectivity of at least about 50%, more preferably at least about 70%, and most preferably at least about 80%. Conversion is preferably about 25% or more and most preferably about 40% or more.

Dehydrochlorination may be carried out at a temperature range of about 200° C. to about 800° C., preferably from about 300° C. to about 600° C., and more preferably from about 400° C. to about 500° C. in the presence of a catalyst. It is contemplated that a variety of reaction pressures may be used, such as superatmospheric, atmospheric, and subatmospheric. Atmospheric pressure is preferred.

Dehydrochlorination may optionally be carried out in presence or absence of an oxidizing agent. Useful examples of oxidizing agents include, but are not limited to, oxygen and carbon dioxide. Use of an oxidizing agent can extend the life of the catalyst. The oxidizing agent can be pure or diluted with an inert gas such as nitrogen before being introduced into reactor. The level of oxidizing agent is generally from about 1% to about 10% by volume and preferably from about 2% to 5% by volume based on the volume of the organic feed.

It may also be advantageous to periodically regenerate the catalyst after prolonged use while in place in the reactor. Regeneration of the catalyst may be accomplished by any means known in the art. One method is by passing oxygen or oxygen diluted with nitrogen over the catalyst at temperatures of about 200° C. to about 600° C. (preferably about 350° C. to about 450° C.) for about 0.5 hour to about 3 days followed by either halogenation treatment at temperatures of about 25° C. to about 400° C. (preferably about 200° C. to about 350° C.) for halogenated metal oxide catalysts and metal halide ones or reduction treatment at temperatures of about 100° C. to about 600° C. (preferably about 200° C. to about 350° C.) for metal catalysts.

Dehydrochlorination is preferably carried out in a corrosion-resistant reaction vessel. Examples of corrosion-resistant materials are Hastelloy, Inconel, Monel and fluoropolymer linings. The vessel may have a fixed or a fluidized catalyst bed. If desired, inert gases such as nitrogen or argon may be employed in the reactor during operation.

Examples

The following are examples of the present invention and are not to be construed as limiting.

Example 1 244bb Dehydrohalogenation Over Metal Fluoride and Fluorinated Metal Oxide Catalysts

A series of mono-, bi-, and tri-valent metal fluorides and fluorinated bi- and tri-valent metal oxides were used as dehydrohalogenation catalysts. Approximately 20 cc of catalyst pellets was used in a typical run. A mixture containing 97.2 wt. % 244bb and 2.0 wt. % 1233xf was passed through the catalyst bed at a rate of 6 g/h at a temperature that ranged from 200° C. to 600° C. The temperatures at the bottom of catalyst bed and at the top of catalyst bed were measured.

As shown in Table 2, NaF, MgF₂, CaF₂, and fluorinated MgO were able to provide a selectivity to 1234yf higher than 80%, while FeF₃ and fluorinated Cr₂O₃ exhibited a selectivity to 1233xf higher than 80%. Selectivity is based on mole percent. These results indicate that mono- and bi-valent metal halides as well as halogenated mono- and bi-valent metal oxides are more favorable than their trivalent counterparts as catalysts for 244bb dehydrochlorination. Among NaF, MgF₂, CaF₂, and fluorinated MgO, MgF₂ exhibited the best performance; it provided a conversion of 244bb above 50% and a selectivity to 1234yf above 85% after 8 h (hours) on stream.

TABLE 2 (Dehydrohalogenation of 244bb over various mono-, bi-, and tri-valent metal fluorides and fluorinated bi- and tri-valent metal oxides*) Temp. Con- Bottom- version Selectivity Selectivity Selectivity Top t 244bb 1234yf 1233xf Unknowns Catalyst (° C.) (h) (%) (%) (%) (%) NaF 450-554 1 24.8 92.2 7.8 450-553 2 22.3 90.3 9.7 450-553 3 19.6 89.6 10.4 450-553 4 15.6 89.1 10.9 450-553 5 12.6 87.4 12.6 fluorinated 450-517 1 25.3 94.6 5.4 MgO 450-517 2 26.5 96.0 4.0 450-518 3 25.8 96.8 3.2 450-518 4 25.4 97.1 2.9 450-516 5 26.6 97.3 2.7 450-516 6 26.3 97.5 2.5 MgF₂ 475-506 1 48.2 76.9 17.7 5.4 475-509 2 52.9 79.8 14.6 5.6 475-509 3 53.3 80.7 12.9 6.4 475-507 4 52.4 81.4 11.9 6.7 475-509 5 54.2 83.0 10.9 6.1 475-510 6 54.1 83.6 10.2 6.2 475-508 7 54.7 84.7 9.6 5.7 475-509 8 53.7 85.4 9.2 5.4 475-510 9 54.9 86.0 8.6 5.5 475-509 10 53.5 86.7 8.2 5.1 CaF₂ 450-511 1 7.0 76.8 23.2 450-510 2 7.3 80.2 19.8 Fluorinated 250-317 1 95.3 6.2 92.6 1.2 Cr₂O₃ 250-316 2 55.0 8.0 89.2 2.8 FeF₃ 350-385 1 90.4 10.9 88.7 0.4 350-385 2 84.7 11.0 88.5 0.5 *Reaction conditions: 20 ml of catalyst, 6 g-organic/h, 97.2% 244bb/2.0% 1233xf, 1 atm

Example 2 244bb Dehydrohalogenation Over Alkaline Metal Chloride-Doped MgF₂ Catalysts

A series of alkaline metal chlorides were investigated as an additive to MgF₂ with a purpose of improving the selectivity to 1234yf. For comparison purpose, the results obtained over MgF₂ catalyst were also reported. Approximately 20 cc of catalyst pellets was used in a typical run. A mixture containing 97.2 wt. % 244bb and 2.0 wt. % 1233xf was passed through catalyst bed at a rate of 6 g/h (grams/hour) at a temperature that ranged from 470° C. to 520° C. The temperatures at the bottom of catalyst bed and at the top of catalyst bed were measured.

As shown in Table 3, the MgF₂ provided a 244bb conversion of 53-55%, a 1234yf selectivity of 80-87%, and a 1233xf selectivity of 8-15%; the 10% LiCl/MgF₂ provided a 244bb conversion below 45%, a 1234yf selectivity of about 90%, and a 1233xf selectivity of about 5%; the 10% KCl/MgF₂ provided a 244bb conversion below 50%, a 1234yf selectivity of about 96%, and a 1233xf selectivity of about 1%; and the 10% CsCl/MgF₂ provided a 244bb conversion of 50-52%, a 1234yf selectivity of about 97%, and essentially no formation of 1233xf. CsCl exhibited the best results, while the 10% CsCl/MgF₂ catalyst provided activity comparable to MgF₂ and the highest 1234yf selectivity while generating no 1233xf.

TABLE 3 (Reactivity of MgF₂ and alkaline metal chloride-doped MgF₂ catalysts during 244bb dehydrohalogenation*) Temp. Con- Select- Bottom- version Selectivity ivity Selectivity, Top t 244bb 1234yf 1233xf Unknowns Catalyst (°) (h) (%) (%) (%) (%) MgF₂ 475-506 1 48.2 76.9 17.7 5.4 475-509 2 52.9 79.8 14.6 5.6 475-509 3 53.3 80.7 12.9 6.4 475-507 4 52.4 81.4 11.9 6.7 475-509 5 54.2 83.0 10.9 6.1 475-510 6 54.1 83.6 10.2 6.2 475-508 7 54.7 84.7 9.6 5.7 475-509 8 53.7 85.4 9.2 5.4 475-510 9 54.9 86.0 8.6 5.5 475-509 10 53.5 86.7 8.2 5.1 10 wt % 475-490 1 29.4 89.1 5.3 5.6 LiCl/MgF₂ 475-506 2 38.8 89.6 5.3 5.0 475-505 3 40.4 89.9 5.2 4.9 475-507 4 42.9 90.5 4.8 4.7 10 wt % 475-514 1 38.3 95.1 0.9 4.0 KCl/MgF₂ 475-515 3 47.2 95.6 0.8 3.6 475-515 5 47.5 95.8 0.7 3.5 475-509 6 43.7 95.8 0.6 3.5 475-514 7 47.1 95.8 0.7 3.5 10 wt % 475-511 1 49.6 96.9 3.1 CsCl/MgF₂ 475-510 2 51.2 97.0 3.0 475-511 3 51.8 96.9 3.1 475-508 4 50.4 96.9 3.1 475-510 5 51.4 97.0 3.0 *Reaction conditions: 20 ml of catalyst, 6 g-organic/h, 97.2% 244bb/2.0% 1233xf, 1 atm

Example 3 244bb Dehydrohalogenation Over CsCl/MgF₂ Catalysts

A series of CsCl/MgF₂ catalysts with different loadings of CsCl were investigated with a purpose of optimizing CsCl loading. 20 cc of catalyst pellets was used in a typical run. A mixture containing 97.2 wt. % 244bb and 2.0 wt. % 1233xf was passed through the catalyst bed at a rate of 6 g/h at a temperature that ranged from 470° C. to 520° C. The temperatures at the top and bottom of the catalyst bed were measured. As shown in Table 4, the selectivity to 1233xf decreased with increasing CsCl loading from 0.0 to 5.0 wt %, and no 1233xf was formed over catalysts with CsCl loadings ≧7.5 wt % based on the total weight of the catalyst.

TABLE 4 (Effect of CsCl loading on the performance of CsCl/MgF₂ catalysts during 244bb dehydrohalogenation*) Temp. CsCl Bottom- Conversion Selectivity Selectivity Selectivity loading Top t 244b 1234yf 1233xf Unknowns (wt. %) (°) (h) (%) (%) (%) (%) 0.0 475-506 1 48.2 76.9 17.7 5.4 475-509 2 52.9 79.8 14.6 5.6 475-509 3 53.3 80.7 12.9 6.4 475-507 4 52.4 81.4 11.9 6.7 475-509 5 54.2 83.0 10.9 6.1 475-510 6 54.1 83.6 10.2 6.2 475-508 7 54.7 84.7 9.6 5.7 475-509 8 53.7 85.4 9.2 5.4 475-510 9 54.9 86.0 8.6 5.5 475-509 10 53.5 86.7 8.2 5.1 2.5 500-514 1 48.4 88.7 5.2 6.1 500-514 2 48.1 88.5 5.2 6.3 500-514 3 49.5 89.1 5.0 5.9 500-507 4 46.9 89.3 4.8 5.9 500-509 5 48.5 89.9 4.6 5.5 500-513 6 48.5 89.6 4.7 5.7 500-514 7 49.6 89.9 4.6 5.5 5.0 490-510 1 49.0 94.8 0.5 4.7 490-511 2 51.0 94.5 0.4 5.1 490-510 3 49.2 95.3 0.5 4.2 490-505 4 48.7 95.0 0.4 4.6 490-507 6 49.8 95.4 0.4 4.2 490-503 8 49.2 95.7 0.4 3.9 7.5 475-510 2 41.9 94.6 5.4 475-507 3 41.6 95.8 4.2 475-508 4 46.1 96.5 3.5 475-506 7 43.5 96.5 3.5 475-506 8 42.2 96.4 3.6 475-507 9 44.0 96.6 3.4 10.0 475-511 1 49.6 96.9 3.1 475-510 2 51.2 97.0 3.0 475-511 3 51.8 96.9 3.1 475-508 4 50.4 96.9 3.1 475-510 5 51.4 97.0 3.0 *Reaction conditions: 20 ml of catalyst, 6 g-organic/h, 97.2% 244bb/2.0% 1233xf, 1 atm

Example 4 244bb Dehydrohalogenation Over Non-Precious Metal-Doped MgF₂ Catalysts

A series of non-precious metals were investigated as additives to MgF₂ with a purpose of improving the selectivity to 1234yf. For comparison purposes, the results obtained over MgF₂ catalyst were also reported. Approximately 20 cc of catalyst pellets was used in a typical run. A mixture containing 97.2 wt. % 244bb and 2.0 wt. % 1233xf was passed through catalyst bed at a rate of 6 g/h at a temperature that ranged from 440 to 540° C. The temperatures at the top and bottom of the catalyst bed were measured.

As shown in Table 5, the addition of cobalt and especially nickel resulted in the decrease in the selectivity to 1233xf, while the addition of iron resulted in an increase in the selectivity to 1233xf. The 12 wt % Ni/MgF₂ catalyst provided a 1234yf selectivity of about 95% with a 1233xf selectivity of about 2%.

TABLE 5 (Reactivity of MgF₂ and metal-doped MgF₂ catalysts during 244bb dehydrohalogenation*) Temp. Con- Bottom- version Selectivity Selectivity Selectivity, Top t 244bb 1234yf 1233xf Unknowns Catalyst (°) (h) (%) (%) (%) (%) MgF₂ 450-529 1 53.5 69.0 26.0 5.0 450-529 2 58.9 74.7 20.8 4.5 450-528 3 60.4 77.9 17.4 4.7 450-530 4 64.5 81.0 14.3 4.7 450-529 5 61.4 82.4 12.9 4.8 450-528 6 62.3 84.3 10.8 4.8 450-529 7 63.7 85.3 9.7 5.0 450-527 8 66.8 86.6 8.6 4.7 450-526 9 64.3 87.0 8.2 4.8 450-530 10 63.5 87.8 7.6 4.5 450-528 11 63.8 88.2 7.2 4.6 450-530 12 64.7 88.3 6.8 4.8 450-528 13 64.1 88.6 6.6 4.8 450-528 14 63.2 89.3 6.2 4.5 12 wt % 450-525 1 71.2 53.4 41.7 4.9 Fe/MgF₂ 450-523 2 72.8 53.0 41.9 5.1 12 wt % 445-527 2 48.5 88.8 7.9 4.3 Co/MgF₂ 445-528 3 58.0 90.1 6.7 3.2 445-528 4 62.8 90.9 5.9 3.2 445-527 5 66.6 91.5 5.2 3.3 12 wt % 445-526 7 54.7 93.0 2.0 5.0 Ni/MgF₂ 445-527 8 53.2 93.4 2.1 4.5 445-526 10 56.2 94.8 2.0 3.2 445-526 11 58.6 94.5 2.0 3.4 *Reaction conditions: 20 ml of catalyst, 6 g-organic/h, 97.2% 244bb/2.0% 1233xf, 1 atm

Example 5 244bb Dehydrohalogenation Over Metal and Metal Alloy Catalysts

A series of supported and unsupported metals as well as metal alloys were used as dehydrohalogenation catalysts. 20 cc of catalyst pellets or a 4 inch-long metal mesh roll was used in a typical run. A mixture containing 97.2 wt. % 244bb and 2.0 wt. % 1233xf was passed through a catalyst bed at a rate of 6 g/h at a temperature ranged from 420° C. to 480° C. The temperatures at the top and bottom of the catalyst bed were measured. As shown in Table 6, all the metal and metal alloy catalysts were active and extremely selective for 244bb dehydrochlorination (1234yf selectivity >95%) while generating no 1233xf. Compared to metal halide and/or halogenated metal oxide catalysts, the metal catalysts did not require as high an operating temperature.

TABLE 6 (reactivity of metal and metal alloys during 244bb dehydrohalogenation*) Temp. Con- Bottom- version Selectivity Selectivity Selectivity, Top t 244b 1234yf 1233xf Unknowns Catalyst (° C.) (h) (%) (%) (%) (%) 5 wt % 450-478 1 43.6 95.3 4.7 Pd/BaSO₄ 450-476 2 30.5 94.6 5.4 450-478 3 30.1 92.9 7.1 450-475 4 29.6 95.1 4.9 450-481 5 31.1 94.8 5.2 Ni mesh 425-473 1 45.8 96.9 3.1 425-473 2 45.5 97.3 2.7 425-473 3 44.8 97.8 2.2 425-473 4 43.7 97.9 2.1 425-473 5 42.1 97.9 2.1 425-473 6 40.5 98.0 2.0 425-472 7 39.5 98.0 2.0 425-473 8 38.6 98.0 2.0 425-473 9 38.6 98.9 1.1 425-474 10 39.2 98.1 1.9 Inconel 425-464 1 26.5 95.8 4.2 600 chips 425-467 2 32.6 97.9 2.1 425-470 3 36.9 98.1 1.9 425-470 4 40.1 98.1 1.9 425-470 5 40.4 98.3 1.7 425-470 6 41.8 98.4 1.6 425-468 7 42.5 98.5 1.5 425-468 8 41.4 98.6 1.4 425-466 9 39.7 98.6 1.4 425-466 10 37.1 98.7 1.3 20cc 425-466 1 25.7 97.3 2.7 Inconel 425-467 2 28.8 97.6 2.4 625 chips 425-467 4 33.4 97.9 2.1 425-459 6 33.8 98.0 2.0 425-465 8 36.2 98.1 1.9 425-463 10 36.8 98.1 1.9 425-465 12 38.0 98.2 1.8 425-465 14 37.7 98.2 1.8 425-462 16 39.1 99.1 0.9 *Reaction conditions: 20 ml of catalyst, 6 g-organic/h, 97.2% 244bb/2.0% 1233xf, 1 atm

It should be understood that the foregoing description is only illustrative of the present invention. Various alternatives and modifications can be devised by those skilled in the art without departing from the invention. Accordingly, the present invention is intended to embrace all such alternatives, modifications and variances that fall within the scope of the appended claims. 

What is claimed is:
 1. A process for making a fluorinated olefin, comprising: dehydrochlorinating a hydrochlorofluorocarbon having at least one hydrogen and at least one chlorine on adjacent carbons in the presence of a catalyst selected from the group consisting of (i) one or more metal halides, (ii) one or more halogenated metal oxides, (iii) one or more zero-valent metals/metal alloys, and (iv) a combination of two or more of these.
 2. The process of claim 1, wherein the hydrochlorofluorocarbon and resulting fluorinated olefin is selected from the group consisting of 1,1,1,2-tetrafluoro-2-chloropropane and 2,3,3,3-tetrafluoropropene, 1,1,1,2-tetrafluoro-3-chloropropane and 2,3,3,3-tetrafluoropropene, 1,1,1,3-tetrafluoro-3-chloropropane and 1,3,3,3-tetrafluoropropene, 1,1,1,3-tetrafluoro-2-chloropropane and 1,3,3,3-tetrafluoropropene, 1,1,1,2,3-pentafluoro-2-chloropropane and 1,2,3,3,3-pentafluoropropene, 1,1,1,2,3-pentafluoro-3-chloropropane and 1,2,3,3,3-pentafluoropropene, 1,1,1,3,3-pentafluoro-3-chloropropane and 1,1,3,3,3-pentafluoropropene, 1,1,1,3,3-pentafluoro-2-chloropropane and 1,1,3,3,3-pentafluoropropene, 1,1,1,2,3,3-hexafluoro-2-chloropropane and 1,1,2,3,3,3-hexafluoropropene, and 1,1,1,2,3,3-hexafluoro-3-chloropropane and 1,1,2,3,3,3-hexafluoropropene.
 3. The process of claim 1, wherein the hydrochlorofluorocarbon is 1,1,1,2-tetrafluoro-2-chloropropane and the fluorinated olefin is 2,3,3,3-tetrafluoropropene.
 4. The process of claim 1, wherein the catalyst is one or more metal halides, wherein one or more metal halides is a mono-valent metal halide, a bi-valent metal halide, a tri-valent metal halide, or a combination of two or more of these.
 5. The process of claim 4, wherein the one or more metal halides has a metal selected from the group consisting of Mg²⁺, Ca²⁺, Ni²⁺, Zn²⁺, Pd²⁺, Li⁺, Na⁺, K⁺, and Cs⁺ and a halogen atom selected from the group consisting of F⁻, Cl⁻, Br⁻, and I⁻.
 6. The process of claim 5, wherein the one or more metal halides is selected from the group consisting of LiF, NaF, KF, CsF, MgF₂, CaF₂, LiCl, NaCl, KCl, CsCl, or a combination of two or more of these.
 7. The process of claim 1, wherein the catalyst is one or more halogenated metal oxides, wherein the one or more halogenated metal oxides is selected from the group consisting of a mono-valent halogenated metal oxide, a bi-valent halogenated metal oxide, a tri-valent halogenated metal oxide, and a combination of two or more of these.
 8. The process of claim 7, wherein the one or more halogenated metal oxides is selected from the group consisting of a mono-valent halogenated metal oxide, a bi-valent halogenated metal oxide, and a combination of two or more of these.
 9. The process of claim 7, wherein the one or more halogenated metal oxides is selected from the group consisting of fluorinated or chlorinated MgO, fluorinated or chlorinated CaO, fluorinated or chlorinated Li₂O, fluorinated or chlorinated Na₂O, fluorinated or chlorinated K₂O, fluorinated or chlorinated Cs₂O, and a combination of two or more of these.
 10. The process of claim 1, wherein the catalyst is one or more zero-valent metals/metal alloys.
 11. The process of claim 10, wherein the one or more zero-valent metals/metal alloys is selected from the group consisting of Pd, Pt, Rh, Fe, Co, Ni, Cu, Mo, Cr, Mn, and combinations of these.
 12. The process of claim 11, wherein the one or more zero-valent metals/metal alloys is selected from the group consisting of Pd, Fe, Co, Ni, and combinations of these.
 13. The process of claim 2, wherein the catalyst is one or more metal halides, wherein the one or more metal halides is selected from the group consisting of a mono-valent metal halide, a bi-valent metal halide, and a combination of two or more of these.
 14. The process of claim 2, wherein the catalyst is one or more halogenated metal oxides, wherein the halogenated metal oxide is selected from the group consisting of a mono-valent halogenated metal oxide, a bi-valent halogenated metal oxide, and a combination of two or more of these.
 15. The process of claim 2, wherein the catalyst is one or more zero-valent metals/metal alloys.
 16. The process of claim 3, wherein the catalyst is one or more metal halides, wherein the one or more metal halides is selected from the group consisting of a mono-valent metal halide, a bi-valent metal halide, and a combination of two or more of these.
 17. The process of claim 3, wherein the catalyst is one or more halogenated metal oxides, wherein the halogenated metal oxide is selected from the group consisting of a mono-valent halogenated metal oxide, a bi-valent halogenated metal oxide, and a combination of two or more of these.
 18. The process of claim 3, wherein the catalyst is a zero-valent metal/metal alloy.
 19. The process of claim 1, wherein the catalyst is a CsCl/MgF₂ combination.
 20. The process of claim 19, wherein the CsCl is about 5.0 wt % to about 50.0 wt % of the combination based on the total weight of the catalyst.
 21. The process of claim 2, wherein the catalyst is a CsCl/MgF₂ combination.
 22. The process of claim 21, wherein the CsCl is about 5.0 wt % to about 50.0 wt % of the combination based on the total weight of the catalyst.
 23. The process of claim 3, wherein the catalyst is a CsCl/MgF₂ combination.
 24. The process of claim 23, wherein the CsCl is about 5.0 wt % to about 50.0 wt % of the combination based on the total weight of the catalyst. 